CN114590973A - System and method for performing efficient denitrification and carbon removal and phosphorus recovery on source separated fresh urine through biochemical combination - Google Patents
System and method for performing efficient denitrification and carbon removal and phosphorus recovery on source separated fresh urine through biochemical combination Download PDFInfo
- Publication number
- CN114590973A CN114590973A CN202210341405.6A CN202210341405A CN114590973A CN 114590973 A CN114590973 A CN 114590973A CN 202210341405 A CN202210341405 A CN 202210341405A CN 114590973 A CN114590973 A CN 114590973A
- Authority
- CN
- China
- Prior art keywords
- reactor
- membrane
- urine
- phosphorus recovery
- denitrification
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/10—Packings; Fillings; Grids
- C02F3/102—Permeable membranes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05B—PHOSPHATIC FERTILISERS
- C05B7/00—Fertilisers based essentially on alkali or ammonium orthophosphates
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/005—Black water originating from toilets
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/40—Liquid flow rate
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F7/00—Aeration of stretches of water
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention provides a system and a method for carrying out efficient denitrification and decarbonization and phosphorus recovery on source separated fresh urine by biochemical combination, and particularly discloses a system which comprises a membrane aeration biomembrane reactor with in-situ denitrification and decarbonization function and subareas, a source separation closestool, a source separated urine storage tank, a phosphorus recovery reactor, a calcium salt solution tank, a water production tank and a control system; the membrane aeration biomembrane reactor is divided into an upper part and a lower part, the upper part forms a micro-aerobic environment, the lower part forms an anaerobic environment, and denitrification and decarbonization can be realized only in the membrane aeration biomembrane reactor. The system provided by the invention can realize more than 95% of denitrification and carbon removal without additionally adding a carbon source, has a small size, and can meet the requirement of in-situ sewage treatment of trains.
Description
Technical Field
The invention belongs to the field of environmental protection, and particularly relates to a system and a method for performing efficient denitrification and carbon removal and phosphorus recovery on source separated fresh urine by biochemical combination.
Background
The existing train toilet collector is only used as a sewage receiving unit and does not have any sewage in-situ treatment function, the sewage quality and the water quantity of the toilet collector are large in fluctuation and the concentration of pollutants is high, the treatment difficulty of the existing treatment method is large, the problems of pollutant residue and biological safety cannot be effectively solved, and excrement sewage and other sewage in a traditional drainage system are mixed, so that more water consumption is caused, pathogens and micro-pollutants in water have diffusion possibility, the pollution load of domestic sewage can be obviously reduced by separating and collecting excrement from the source, the treatment difficulty of a sewage treatment plant is reduced, and the risk of polluting water bodies by pollutant discharge is reduced. Research shows that the average daily urine output of each person is 1.5L, which only accounts for 2% of the daily domestic sewage discharge amount, but contributes 90% of nitrogen, 50% of phosphorus and 10% of COD in the domestic sewage, so that the source separation of the excrement and the urine becomes an environmental protection trend. The treatment of the fresh urine of source separation also has obvious advantage for source separation hydrolysis urine in addition, on the one hand to the source separation urine that train etc. need the normal position to be handled, if increase the storage device that urea hydrolysises not only increase construction cost, increase the space burden moreover, on the other hand hydrolysis urine can produce pungent smell because the volatilization of ammonia etc. produces, produces harmful effects to the external world, if increase the processing of removing the flavor and increase the running cost equally. Therefore, the efficient treatment of the source separated fresh urine has profound significance, after the source separated fresh urine is subjected to denitrification and carbon removal and phosphorus recovery, the treated water is used for flushing a toilet, so that not only are water resources saved, but also valuable resources such as phosphorus and the like can be recovered, and the cyclic utilization of energy is realized.
In the prior art, doctor thesis 1, "yellow water resource treatment technology research based on phosphorus and potassium recovery" mentions a yellow water resource treatment technology, wherein a nitrosation-anaerobic ammonia oxidation method is adopted, SBR is used as a carrier for denitrification treatment, and the deamination rate of the yellow water treated by the method reaches over 90 percent. It is also noted that pretreatment for organic removal eliminates the potential effect of organic removal due to the high proportion of organic present in the yellow water.
In the prior art 2CN 113845224 a, a process method suitable for low carbon nitrogen ratio sewage treatment is mentioned, and a process method suitable for low carbon nitrogen ratio sewage treatment is provided, which improves the synergistic denitrification performance of key functional bacteria in an MABR biomembrane by establishing a partial shortcut nitrification-anaerobic ammonia oxidation membrane aeration biomembrane reactor (PN/a MABR). Has the advantages of low energy consumption, low sludge yield and the like, can replace partial functions of an aerobic pool, an anoxic pool and an anaerobic pool of the traditional biological denitrification process, and reduces the number and the area of structures.
The prior art 3CN 113184818A source separated urine high-purity nitrogen and phosphorus recovery device, recovery method and application thereof, and researches on the development of a plurality of technologies by researchers to realize the separation and recovery of nitrogen and phosphorus in source separated urine are provided, and the most widely used method is a chemical precipitation method, so that a nitrogen and phosphorus-containing slow release fertilizer, such as struvite (MgNH)4PO4·6H2O) and hydroxyapatite [ Ca5(PO4)3OH]. It also addresses the problem of not only requiring additional chemicals (e.g., magnesium source, calcium source or alkali) to provide optimal precipitation conditions, resulting in increased overall cost, but also coexistence of high concentrations of ions such as HCO3-、Na+、K+And Ca2+Can induce the production of undesirable mineral components in the source separated urine, and greatly reduce the quality of the obtained nitrogen and phosphorus products.
However, the prior art methods do not meet the need to achieve in situ recovery, disposal and reuse of the source separated urine.
Disclosure of Invention
In order to solve the problems, the invention provides a system and a method for carrying out high-efficiency denitrification and carbon removal and phosphorus recovery on fresh urine separated from a source by biochemical combination. The system has small volume and high treatment efficiency, and the obtained sewage can be recycled after in-situ treatment without adding extra carbon sources.
One aspect of the invention provides a functional-partitioning membrane-aeration biofilm reactor (MABR) for in-situ denitrification and decarbonization, which comprises a vertically arranged box body, wherein the box body comprises an upper part and a lower part, the upper part is provided with an MABR membrane component, and the lower part is a space communicated with the upper part; the box body is provided with a first water inlet, a first water outlet and a backflow port, and the first water inlet is arranged at the bottom of the membrane aeration biomembrane reactor of the functional partition; the first water outlet is arranged at the upper part of the membrane aeration biomembrane reactor of the functional partition and is not lower than the MABR membrane component; the membrane aeration biomembrane reactor with the function division is also provided with a backflow port, and the backflow port is connected with the first water inlet through a backflow pump; and an aeration device for providing oxygen for the MABR membrane component is arranged at the top of the membrane aeration biomembrane reactor with the functional zones.
Further, the first water outlet is arranged above the MABR membrane module.
Further, a second liquid flow meter is provided upstream of the reflux pump.
Furthermore, anaerobic bacteria are arranged in the lower part of the membrane-aeration biomembrane reactor of the functional partition, and microorganisms of a nitrosation-anaerobic ammonia oxidation double-bacteria layer are attached to the MABR membrane component on the upper part of the membrane-aeration biomembrane reactor of the functional partition.
Furthermore, denitrifying bacteria are also arranged in the lower part of the MABR functional zone reactor.
Further, the volume of the upper part of the MABR function zone reactor is 30-50L, and the volume of the lower part of the MABR function zone reactor is 20-30L.
In another aspect, the invention provides a method for denitrogenating and decarbonizing source separated urine, which comprises the step of treating the source separated urine with the in-situ denitrogenating and decarbonizing MABR functional zone reactor.
Further, the method comprises:
s01) injecting fresh urine separated from a source into the lower part of the membrane-aeration biomembrane reactor of the functional partition through a first water inlet, and adjusting the dissolved oxygen concentration at the lower part of the membrane-aeration biomembrane reactor to be 0 through an aeration device to realize that urea is hydrolyzed into ammonia nitrogen under the action of anaerobic bacteria;
s02) after the hydrolysis rate of urea at the middle and lower parts reaches more than 85% in the step S01), continuously injecting fresh urine to be treated through a first water inlet at the bottom, enabling part of the urine to enter an upper MABR membrane module, controlling the dissolved oxygen of the upper MABR membrane module to be 0.3-0.5mg/L, and denitrifying under the action of microorganisms on the surface of the upper MABR membrane module to generate nitrogen and nitrate nitrogen;
s03) refluxing the liquid containing the nitrate and the nitrogen after the upper treatment to the lower part of the membrane aeration biomembrane reactor through a reflux pump, and reducing the nitrate and the nitrogen into nitrogen through denitrification at the lower part.
In another aspect, the invention provides a system for performing efficient denitrification and decarbonization and phosphorus recovery on source separated fresh urine, which comprises the in-situ denitrification and decarbonization functional partitioned membrane-aerated biofilm reactor.
Further, the system also comprises a source separation toilet, a source separation urine storage tank, a phosphorus recovery reactor, a calcium salt solution tank, a water production tank and a control system;
the source separation closestool is arranged between the source separation closestool and the source separation urine storage tank, between the source separation urine storage tank and the membrane aeration biomembrane reactor of the functional partition, and between the membrane aeration biomembrane reactor of the functional partition and the phosphorus recovery reactor; the phosphorus recovery reactors are connected with the water production tanks, the phosphorus recovery reactors are connected with the calcium salt solution tank, and the water production tank is connected with the source separation closestool through pipelines, and at least one of a valve, a water pump and a liquid flow meter is configured;
the flow direction and the flow rate of the liquid in the pipeline and the aeration quantity are controlled by a control system.
Further, a second water inlet, a second water outlet, a calcium phosphate collecting port, a stirring device and a calcium salt feeding port are arranged on the phosphorus recovery reactor; the calcium phosphate collecting port is arranged at the bottom of the phosphorus recovery reactor, the second water inlet and the second water outlet are arranged on the side wall of the phosphorus recovery reactor, and the position of the second water inlet is lower than that of the second water outlet.
Further, the calcium salt addition port is provided at the top of the phosphorus recovery reactor.
Further, the calcium salt solution tank controls the calcium salt solution to be added into the phosphorus recovery reactor through a calcium adding pump and a liquid flow meter.
Further, the liquid part obtained after the source separation closestool is separated is connected with the source separation urine storage tank through a pipeline, and the water production tank is connected with the flushing water phase of the source separation closestool through a pipeline.
In yet another aspect, the present invention provides a method for efficient denitrification and carbon removal and phosphorus recovery of fresh urine from a source separation, the method comprising the steps of:
s11), separating the urine by a source separation closestool, then feeding the urine into a source separation urine storage tank, and injecting the urine into a membrane aeration biomembrane reactor with a function partition according to the required flow to perform denitrification and decarbonization treatment;
s12) the effluent after denitrification and decarbonization treatment by the membrane-aeration biomembrane reactor with the function partition enters a phosphorus recovery reactor, and meanwhile, a calcium salt solution is added into the phosphorus recovery reactor, the mass concentration of calcium contained in the calcium salt solution is about 3 times of the phosphorus concentration in the effluent of the membrane-aeration biomembrane reactor with the function partition in the step S11), and hydroxyapatite precipitate is formed under the slow mixing of a stirring device;
s13), discharging sludge through a calcium phosphate collecting port at the bottom of the phosphorus recovery reactor to recover phosphorus in urine, and returning the supernatant after phosphorus removal to a water production tank of a source separation closestool;
the method for carrying out denitrification and decarbonization treatment on the membrane-aeration biomembrane reactor with the function zones in the step S11) comprises the following steps:
s01) injecting fresh urine separated from a source into the lower part of the membrane-aeration biomembrane reactor of the functional partition through a first water inlet, and adjusting the dissolved oxygen concentration at the lower part of the membrane-aeration biomembrane reactor to be 0 through an aeration device to realize anaerobic hydrolysis of urea into ammonia nitrogen;
s02) after the hydrolysis rate of urea at the middle and lower parts reaches more than 85% in the step S01), continuously injecting fresh urine to be treated through a first water inlet at the bottom, enabling part of the urine to enter an upper MABR membrane module, controlling the dissolved oxygen of the upper MABR membrane module to be 0.3-0.5mg/L, and denitrifying under the action of microorganisms on the surface of the upper MABR membrane module to generate nitrogen and nitrate nitrogen;
s03) refluxing the liquid containing the nitrate and the nitrogen after the upper treatment to the lower part of the membrane aeration biomembrane reactor through a reflux pump, and reducing the nitrate and the nitrogen into nitrogen through denitrification at the lower part.
In step S11-13), the reaction temperature is 30 +/-1 ℃, the pH is 7.4-8.1, and the Hydraulic Retention Time (HRT) is 5-10 hours.
Advantageous effects
The system of the invention adopts the MABR membrane component for aeration, the membrane component has high oxygen transfer efficiency and can reduce the electric quantity consumed when the aeration quantity is increased, and the membrane component carries out bubble-free aeration, can reduce the volatilization of volatile gas in urine and reduce the adverse effect on the outside, the DO partition is realized by arranging the MABR on the upper part of the membrane aeration biomembrane reactor (reactor A), the micro-aerobic environment can be formed on the upper part of the reactor A, the anaerobic environment is formed on the lower part of the reactor A, so that different microorganisms can form dominant microorganisms on the upper and lower areas of the reactor A, the denitrification and the decarbonization can be realized only in the reactor A, the hydroxyapatite formed in the reactor B can be recycled as a material for producing, in addition, the phosphorus fertilizer after the denitrification and the dephosphorization are recycled can be used for flushing a toilet, and the use of tap water is reduced, realizing the reclamation of urine.
The invention realizes a processing system with smaller size, and can meet the requirement of separating urine from a train in-situ processing source.
According to the scheme of the invention, more than 95% of denitrification and carbon removal can be realized without additionally adding a carbon source.
Drawings
Fig. 1 is a schematic diagram of a system for performing high-efficiency denitrification, carbon removal and phosphorus recovery on source separated fresh urine by using a biochemical combination, wherein 1 is a source separated toilet bowl, 2 is a source separated urine storage tank, 3 is a water inlet pump, 4 is a first liquid flow meter, 5 is a first water inlet, 6 is a return port, 7 is a second liquid flow meter, 8 is a return pump, 9 is a control system, 10 is an air blower, 11 is an air flow meter, 12 is an MABR membrane module, 13 is a first water outlet, 14 is a reactor a, 15 is a calcium phosphate collection port, 16 is a second water inlet, 17 is a reactor B, 18 is a second water outlet, 19 is a water production tank, 20 is a calcium chloride solution tank, 21 is a calcium adding pump, 22 is a third liquid flow meter, and 23 is a stirrer.
Detailed Description
In order to make the aforementioned objects, features and advantages of the present invention more comprehensible, specific embodiments thereof are described in detail below, but the present invention is not to be construed as being limited to the implementable range thereof.
Example 1
As shown in fig. 1, a system for performing high-efficiency denitrification, carbon removal and phosphorus recovery on source separated fresh urine by biochemical combination comprises a source separation toilet 1, a source separated urine storage tank 2, an MABR functional zone reactor (reactor a)14, a phosphorus recovery reactor (reactor B)17, a water production tank 19 and a control system 9;
the MABR functionally-partitioned reactor (reactor a)14 is provided with a first water inlet 5, a first water outlet 13, a MABR membrane module 12, a return port 6, and aeration means including a blower 10 and an air flow meter 11. The MABR membrane module 12 is arranged at the upper part of the MABR function zone reactor 14, and the lower part of the MABR membrane module 12 is provided with a space capable of containing liquid and used for hydrolyzing urea without oxygen; the first water inlet 5 is arranged at the bottom of the MABR functional zone reactor 14; the first water outlet is arranged at the upper part of the MABR function zone reactor 14, is not lower than the MABR membrane module 12, and is preferably arranged above the MABR membrane module 12. The MABR functional zone reactor 14 is also provided with a return port 6, the return port 6 is connected with the first water inlet 5 through a return pump 8, and the upstream of the return pump 8 is also provided with a second liquid flow meter 7; the aeration equipment aerates the MABR membrane module 12 through the top of the MABR functional zone reactor.
The phosphorus recovery reactor (reactor B)17 comprises a stirring device and a calcium adding device, and the stirring device is a stirrer 23; the calcium addition device comprises a calcium chloride solution tank 20 for adding calcium salt to the phosphorus recovery reactor (reactor B) via a calcium addition pump 21 and a third liquid flow meter 22. The phosphorus recovery reactor (reactor B) is also provided with a second water inlet 16, a second water outlet 18 and a calcium phosphate collecting port 15; the calcium phosphate collecting port is arranged at the bottom of a phosphorus recovery reactor (reactor B) 17; the second water inlet 16 is arranged at the lower part of the second water outlet 18; the calcium addition device adds calcium salt through the top of the phosphorus recovery reactor (reactor B) 17.
After the source separation closestool 1 is subjected to source separation, a liquid part is connected to a source separation urine storage tank 2 through a pipeline, the separation urine storage tank 2 is connected with a first water inlet 5 of an MABR function zone reactor (reactor A)14 through a water inlet pump 3 and a first liquid flow meter 4, and a first water outlet arranged on the MABR function zone reactor (reactor A)14 is connected with a second water inlet 16 of the phosphorus recovery reactor (reactor B) through a pipeline; the second water outlet 18 of the phosphorus recovery reactor (reactor B) is connected with a water production tank 19 through a pipeline, and the water production tank 19 is connected with the source separation closestool 1 through a pipeline.
The control system 9 controls the opening and closing of aeration and the aeration amount by controlling the blower 10, the opening and closing of reflux and the reflux flow rate by controlling the reflux pump 8, the opening and closing of calcium addition and the calcium addition amount by controlling the calcium addition pump 21, and the opening and closing of stirring and the stirring speed by controlling the stirrer. The water inlet pump 3 is controlled to control the flow direction and the flow rate of liquid in the pipeline.
In some specific embodiments, water pumps are arranged between the source separation toilet 1 and the source separation urine tank 2, between the first water outlet 13 and the second water inlet 16, between the second water outlet 18 and the water production tank 19 and/or between the water production tank 19 and the source separation toilet 1, and can be controlled by the control system 9 respectively.
The invention is designed aiming at the problem that the existing train toilet bowl is only used as a sewage receiving unit and does not have any sewage in-situ treatment function. The system designed by the invention can be used for solving the problems that the existing treatment method is difficult to realize high standard discharge requirement and the like aiming at the sewage characteristics of train toilet bowls, namely large water quality and water quantity fluctuation, high pollutant concentration and the like, and can realize in-situ sewage treatment and recovery in a compact space of a train. Through detection, the water quality of the treated effluent meets the discharge limit of discharge Standard of pollutants for municipal wastewater treatment plant (GB18918-2002) A by the method for efficiently removing nitrogen, carbon and phosphorus from the source separated fresh urine by biochemical combination provided by the invention.
TABLE 1
As shown in figure 1, in the system and the method for performing high-efficiency denitrification, carbon removal and phosphorus recovery on source separated fresh urine by biochemical combination, the source separation closestool 1 is used for separating excrement and urine at a source and realizing independent storage and treatment; a source-separated urine storage tank 2 for storing source-separated urine to provide sufficient influent water for the treatment device; the lower part of the MABR functional zone reactor (reactor A) is an anaerobic environment, urea hydrolysis and denitrification removal of COD in urine and nitrate nitrogen generated at the upper part are realized in the area; the upper part of an MABR functional zone reactor (reactor A) realizes micro aerobic environment through bubble-free aeration, denitrification is realized in the area through integrated PN/A, a small amount of generated nitrate nitrogen flows back to the lower part of the reactor through a reflux pump, and deep denitrification is carried out through denitrification; the phosphorus recovery reactor (reactor B) is a device for recovering phosphorus from the denitrified and decarbonized source separated urine by adding a calcium chloride solution; effluent water subjected to denitrification and carbon removal and phosphorus recovery by the reactor A and the reactor B is stored in a water production tank and is used for separating a source and flushing a closestool.
In the system and the method for efficiently removing nitrogen, carbon and phosphorus from fresh urine separated by biochemical combination, the reactor A is subjected to bubble-free aeration by the MABR, the oxygen transfer efficiency is high, the power consumption is low, the influence on volatile substances in water is small, hydroxyapatite generated by the reactor B can be used as a raw material for producing phosphate fertilizer, effluent treated by the system can be used for flushing toilets, and the use of tap water is reduced.
In order to realize the in-situ treatment of sewage in a limited space of a train and realize the recycling of the treated water, the system is arranged in a reactor A with the volume of 30L, a reactor B with the volume of 20L, a source separation urine storage tank with the volume of 50L and a production water tank with the volume of 100L.
On the premise of not additionally adding organic matters, the device realizes the effect of in-situ treatment of the yellow water, the urea removal proportion reaches more than 98 percent, and the treated water can reach the degree of back flow flushing of the closestool. The whole set of device is small in size and can be used on a train.
The system and the method for efficiently denitrifying and decarbonizing fresh urine and recovering phosphorus by biochemical combination realize automatic control of a reflux pump, a water pump, an aeration facility and the like.
Example 3:
as shown in FIG. 1, a system and method for high-efficiency denitrification, carbon removal and phosphorus recovery of fresh urine from source separation by biochemical combination comprises the following steps;
step 1, separating the produced urine by a source separation closestool, then feeding the separated urine into a source separation urine storage tank, and feeding the separated urine into the lower part of a reactor A by a water inlet pump according to the required flow;
step 2, hydrolyzing urea contained in the fresh urine entering the lower part of the reactor A in an anaerobic environment into ammonia nitrogen under the action of microorganisms, and carrying out integrated partial nitrosation/anaerobic ammonia oxidation (PN/A) reaction on the generated ammonia nitrogen through an MABR membrane component on the upper part of the aerobic reactor A to generate nitrogen and partial nitrone;
3, introducing the nitrate nitrogen generated at the upper part of the reactor A into the lower part of the reactor A through a reflux pump, and reducing the nitrate nitrogen into nitrogen by using organic matters in urine by denitrifying bacteria at the lower part to realize carbon removal and deep denitrification;
step 4, the effluent after denitrification and decarbonization treatment of the reactor A enters a reactor B, and a calcium chloride solution is added into the reactor B, wherein the mass concentration of calcium contained in the calcium chloride solution is about 3 times of the phosphorus concentration in the effluent of the reactor A, and hydroxyapatite precipitate is formed under the slow mixing of a stirrer;
and 5, discharging sludge from the lower part of the reactor B to recover phosphorus in urine, and feeding the supernatant after removing phosphorus in the reactor B into a water production tank for flushing a source separation closestool.
In the step 1, the urine is discharged to a source separation closestool, then enters a source separation urine storage tank after being flushed by about 0.5L of clear water in a production water tank, and then the flow of a water inlet pump is controlled according to the Hydraulic Retention Time (HRT) of the reactor A, wherein the HRT is 6-10 h.
In the step 2, the flow rate of air of an upper MABR of the reactor A is adjusted to control the upper Dissolved Oxygen (DO) to be 0.3-0.5mg/L, the lower DO is 0, the hydrolysis rate of urea in fresh urine is above 85% under the action of lower anaerobes, the rest urea enters an aerobic MABR area, the urea is further hydrolyzed into ammonia nitrogen under the action of microorganisms in the area, the ammonia nitrogen generated by urea hydrolysis in the two areas is treated by integrated PN/A microorganisms attached to an MABR membrane component to generate nitrogen and partial nitrate nitrogen, the removal rate of the ammonia nitrogen in the area is above 90%, and the removal rate of the nitrate nitrogen generated by the integrated PN/A is about 11% of the removal rate of the ammonia nitrogen.
In the step 3, nitrate nitrogen generated by the integral PN/A at the upper part of the reactor A flows back to the lower part of the reactor A through a reflux pump, a liquid flow meter is adjusted according to the removal condition of the nitrate nitrogen, the reflux flow is controlled, denitrifying bacteria in the area reduce the nitrate nitrogen into nitrogen through denitrification by taking COD in urine as an organic carbon source, the removal rate of the nitrate nitrogen in the area is more than 85%, and the removal rate of the COD is more than 90% under the synergistic action of the denitrifying bacteria and other anaerobic heterotrophic bacteria, so that the decarbonization and the deep denitrification are realized at the lower part of the reactor A.
And 4, the urine subjected to denitrification and decarbonization treatment by the reactor A enters a reactor B through a water outlet 1, a calcium chloride solution is added into the reactor B, the addition amount of the calcium chloride solution is controlled by a liquid flowmeter, the mass concentration of calcium contained in the calcium chloride solution is about 3 times of the mass concentration of phosphorus in the effluent of the reactor A, the calcium and the phosphorus are slowly stirred by a stirrer to only play a role, and the calcium and the phosphorus are slowly mixed by the stirrer to react to form hydroxyapatite precipitate and sink to the lower part of the reactor B.
And 5, discharging sludge from the lower part of the reactor B to recover phosphorus in urine, wherein the hydroxyapatite precipitate deposited at the lower part of the reactor B can be used as a raw material for producing a phosphate fertilizer, the phosphorus removal rate in the reactor is over 80 percent, and the supernatant obtained after phosphorus removal in the reactor B enters a water production tank through a water outlet 2 and is used for flushing a source separation closestool to realize resource utilization of the urine.
As described above, although the embodiments of the present invention have been described in detail, it will be apparent to those skilled in the art that many modifications are possible without substantially departing from the spirit and scope of the present invention. Therefore, such modifications are also all included in the scope of protection of the present invention.
The existing train toilet wastewater collector in China is only used as a sewage receiving unit and does not have any sewage in-situ treatment and recycling functions, the existing toilet wastewater collector is mainly treated in a centralized way by a unified sewage discharge + direct discharge municipal pipe network or sewage discharge + station section sewage treatment station, and the method belongs to a typical high-energy-consumption pollutant end treatment mode. In addition, in the invention, the fresh urine separated from the source is subjected to in-situ treatment to remove carbon and nitrogen in the urine and recover phosphorus, and the treated produced water is used for flushing toilets, so that the urine is recycled, and the use of flushing tap water by trains can be reduced.
Claims (10)
1. A membrane-aeration biofilm reactor with function zoning for in-situ denitrification and decarbonization is characterized by comprising a vertically arranged box body, wherein the box body comprises an upper part and a lower part, the upper part is provided with an MABR membrane component, and the lower part is a space communicated with the upper part; the box body is provided with a first water inlet, a first water outlet and a backflow port, and the first water inlet is arranged at the bottom of the membrane aeration biomembrane reactor of the functional partition; the first water outlet is arranged at the upper part of the membrane aeration biomembrane reactor of the functional partition and is not lower than the MABR membrane component; the membrane aeration biomembrane reactor with the function division is also provided with a backflow port, and the backflow port is connected with the first water inlet through a backflow pump; the top of the membrane aeration biomembrane reactor with the functional subareas is provided with an aeration device for providing oxygen for the MABR membrane component;
preferably, the first water outlet is arranged above the MABR membrane module;
preferably, a second liquid flow meter is also arranged upstream of the reflux pump;
preferably, anaerobic bacteria are arranged in the lower part of the membrane-aeration biomembrane reactor of the functional partition, and microorganisms of a nitrosation-anaerobic ammonia oxidation double bacterial layer are attached to an MABR membrane component on the upper part of the membrane-aeration biomembrane reactor of the functional partition;
preferably, denitrifying bacteria are also arranged in the lower part of the MABR functional zone reactor.
2. The membrane-aerated biofilm reactor of claim 1, wherein the MABR functionally zoned reactor has an upper volume of 30 to 50 liters and a lower volume of 20 to 30 liters.
3. A method for removing nitrogen and carbon from source separated urine, which comprises the step of treating the source separated urine with the membrane-aerated biofilm reactor of the functional partition of claim 1 or 2;
preferably, the method comprises:
s01) injecting urine separated from a source into the lower part of the membrane-aeration biomembrane reactor of the functional partition through a first water inlet, and adjusting the dissolved oxygen concentration at the lower part of the membrane-aeration biomembrane reactor to be 0 through an aeration device to realize that urea is hydrolyzed into ammonia nitrogen under the action of anaerobic bacteria;
s02) after the hydrolysis rate of urea at the middle and lower parts reaches more than 85% in the step S01), continuously injecting urine to be treated through a first water inlet at the bottom, enabling part of the urine to enter an upper MABR membrane module, controlling the dissolved oxygen of the upper MABR membrane module to be 0.3-0.5mg/L, and denitrifying under the action of microorganisms on the surface of the upper MABR membrane module to generate nitrogen and nitrone;
s03) refluxing the liquid containing the nitrate and the nitrogen after the upper treatment to the lower part of the membrane aeration biomembrane reactor through a reflux pump, and reducing the nitrate and the nitrogen into nitrogen through denitrification at the lower part.
4. A system for high efficiency denitrification carbon removal and phosphorus recovery from fresh urine from a source separation, comprising the functionally partitioned membrane-aerated biofilm reactor of claim 1 or 2;
preferably, the system further comprises a source separation toilet, a source separation urine storage tank, a phosphorus recovery reactor, a calcium salt solution tank, a water production tank, and a control system.
5. The system for denitrification decarbonization and phosphorus recovery with high efficiency for fresh urine separated from source as claimed in claim 4, wherein the system is characterized in that the system is arranged between the source separation toilet and the source separation urine storage tank, between the source separation urine storage tank and the membrane-aerated biofilm reactor with functional partition, or between the membrane-aerated biofilm reactor with functional partition and the phosphorus recovery reactor; the phosphorus recovery reactors are connected with the water production tank, the phosphorus recovery reactors are connected with the calcium salt solution tank, and the water production tank is connected with the source separation closestool through pipelines, and at least one of a valve, a water pump and a liquid flow meter is configured;
the flow direction and the flow speed of the liquid in the pipeline and the aeration amount are controlled by a control system.
6. The system for high efficiency denitrification carbon removal and phosphorus recovery for fresh urine from source separation as claimed in claim 4, wherein the phosphorus recovery reactor is provided with a second water inlet, a second water outlet, a calcium phosphate collection port, a stirring device and a calcium salt inlet; the calcium phosphate collecting port is arranged at the bottom of the phosphorus recovery reactor, the second water inlet and the second water outlet are arranged on the side wall of the phosphorus recovery reactor, and the position of the second water inlet is lower than that of the second water outlet.
7. The system for high efficiency denitrification carbon removal and phosphorus recovery for fresh urine from source separation as claimed in claim 4, wherein said calcium salt inlet is placed at the top of the phosphorus recovery reactor;
the calcium salt solution tank controls the calcium salt solution to be added into the phosphorus recovery reactor through a calcium adding pump and a liquid flowmeter;
the liquid part obtained after the source separation closestool is separated is connected with the source separation urine storage tank through a pipeline, and the water production tank is connected with the flushing water phase of the source separation closestool through a pipeline.
8. A method for the efficient denitrification of carbon and phosphorus recovery from source separated fresh urine, said method comprising the steps of treating with the system of any of claims 4-7;
preferably, the method comprises the steps of:
s11), separating the urine by a source separation closestool, then feeding the urine into a source separation urine storage tank, and injecting the urine into a membrane aeration biomembrane reactor with a function partition according to the required flow to perform denitrification and decarbonization treatment;
s12) the effluent after denitrification and decarbonization treatment by the membrane-aeration biomembrane reactor with the function partition enters a phosphorus recovery reactor, and meanwhile, a calcium salt solution is added into the phosphorus recovery reactor, the mass concentration of calcium contained in the calcium salt solution is about 3 times of the phosphorus concentration in the effluent of the membrane-aeration biomembrane reactor with the function partition in the step S11), and hydroxyapatite precipitate is formed under the slow mixing of a stirring device;
s13), discharging sludge through a calcium phosphate collecting port at the bottom of the phosphorus recovery reactor to recover phosphorus in urine, and returning the supernatant after phosphorus removal to a water production tank of the source separation closestool.
9. The method of claim 8, wherein the reaction temperature is 30 ± 1 ℃, the pH is 7.4-8.1, and the hydraulic retention time is 5-10 hours in step S11-13).
10. The method for denitrification and decarbonization and phosphorus recovery with high efficiency for fresh urine separated from source according to claim 8 or 9, wherein the denitrification and decarbonization treatment in the membrane-aerated biofilm reactor with functional partition in the step S11) comprises the following steps:
s01) injecting fresh urine separated from a source into the lower part of the membrane-aeration biofilm reactor with the functional zones in the claim 1 or 2 through a first water inlet, and adjusting the dissolved oxygen concentration at the lower part of the membrane-aeration biofilm reactor to be 0 through an aeration device to realize anaerobic hydrolysis of urea into ammonia nitrogen;
s02) after the hydrolysis rate of urea at the middle and lower parts reaches more than 85% in the step S01), continuously injecting fresh urine to be treated through a first water inlet at the bottom, enabling part of the urine to enter an upper MABR membrane module, controlling the dissolved oxygen of the upper MABR membrane module to be 0.3-0.5mg/L, and denitrifying under the action of microorganisms on the surface of the upper MABR membrane module to generate nitrogen and nitrate nitrogen;
s03) refluxing the liquid containing the nitrate and the nitrogen after the upper treatment to the lower part of the membrane aeration biomembrane reactor through a reflux pump, and reducing the nitrate and the nitrogen into nitrogen through denitrification at the lower part.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210341405.6A CN114590973B (en) | 2022-04-02 | 2022-04-02 | System and method for performing high-efficiency denitrification, carbon removal and phosphorus recovery on source separation fresh urine through biochemical combination |
| US18/194,853 US20230312382A1 (en) | 2022-04-02 | 2023-04-03 | System and method for efficient nitrogen and carbon removal and phosphorus recovery of source-separated fresh urine by biochemical combination |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210341405.6A CN114590973B (en) | 2022-04-02 | 2022-04-02 | System and method for performing high-efficiency denitrification, carbon removal and phosphorus recovery on source separation fresh urine through biochemical combination |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114590973A true CN114590973A (en) | 2022-06-07 |
| CN114590973B CN114590973B (en) | 2023-09-26 |
Family
ID=81821779
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210341405.6A Active CN114590973B (en) | 2022-04-02 | 2022-04-02 | System and method for performing high-efficiency denitrification, carbon removal and phosphorus recovery on source separation fresh urine through biochemical combination |
Country Status (2)
| Country | Link |
|---|---|
| US (1) | US20230312382A1 (en) |
| CN (1) | CN114590973B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117263289A (en) * | 2023-11-10 | 2023-12-22 | 北京工业大学 | Distributed treatment system and method for recycling nutrition of source separation urine |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1052696A (en) * | 1996-08-09 | 1998-02-24 | Ebara Corp | Method for combined treatment of human waste and private sewerage plant sludge |
| CN101439915A (en) * | 2008-12-25 | 2009-05-27 | 同济大学 | Membrane aeration biomembrane process and apparatus for sewerage short-cut denitrification |
| CN103732546A (en) * | 2011-06-01 | 2014-04-16 | 香港科技大学 | Method for wastewater treatment by urine separation, seawater addition, and nitrification and in-sewer denitrification |
| CN111606419A (en) * | 2020-06-01 | 2020-09-01 | 北京工业大学 | Sewage treatment system and method with self-sufficient energy |
| CN214653941U (en) * | 2021-02-02 | 2021-11-09 | 中国科学院生态环境研究中心 | Integrated nitrogen and phosphorus removal sewage treatment device |
-
2022
- 2022-04-02 CN CN202210341405.6A patent/CN114590973B/en active Active
-
2023
- 2023-04-03 US US18/194,853 patent/US20230312382A1/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1052696A (en) * | 1996-08-09 | 1998-02-24 | Ebara Corp | Method for combined treatment of human waste and private sewerage plant sludge |
| CN101439915A (en) * | 2008-12-25 | 2009-05-27 | 同济大学 | Membrane aeration biomembrane process and apparatus for sewerage short-cut denitrification |
| CN103732546A (en) * | 2011-06-01 | 2014-04-16 | 香港科技大学 | Method for wastewater treatment by urine separation, seawater addition, and nitrification and in-sewer denitrification |
| CN111606419A (en) * | 2020-06-01 | 2020-09-01 | 北京工业大学 | Sewage treatment system and method with self-sufficient energy |
| CN214653941U (en) * | 2021-02-02 | 2021-11-09 | 中国科学院生态环境研究中心 | Integrated nitrogen and phosphorus removal sewage treatment device |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117263289A (en) * | 2023-11-10 | 2023-12-22 | 北京工业大学 | Distributed treatment system and method for recycling nutrition of source separation urine |
Also Published As
| Publication number | Publication date |
|---|---|
| US20230312382A1 (en) | 2023-10-05 |
| CN114590973B (en) | 2023-09-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100398470C (en) | Infiltration method for treating garbage | |
| CN101357812B (en) | Processing method for domestic garbage leachate | |
| CN101244883B (en) | High-efficiency low-consumption retexture method for urban sewage | |
| CN100545110C (en) | Dispose of sewage or the micro-polluted raw packaging stage-type film bioreactor device | |
| CN105330108B (en) | Utilize anaerobism-catalytic oxidation biofilm reactor processing sanitary sewage method and processing unit | |
| CN207330633U (en) | A kind of utilization system of high-ammonia nitrogen low C OD waste water | |
| CN204897650U (en) | Chemistry pharmacy effluent disposal system | |
| CN114291964B (en) | Sewage treatment system and method for denitrification and phosphorus recovery | |
| CN105060627A (en) | Chemical pharmacy wastewater comprehensive treatment system | |
| CN111646649A (en) | Excrement wastewater treatment method for modular railway train excrement collector | |
| CN105060598A (en) | Chemical pharmacy wastewater pretreatment system | |
| CN111646648B (en) | Remote treatment method for excrement and urine wastewater of modularized railway train excrement and urine collector | |
| CN102491597B (en) | Method for treating high-concentration nitrogenous organic wastewater | |
| CN106045030B (en) | A2The apparatus and method of/O-UASB continuous flow city domestic sewage advanced nitrogen dephosphorization | |
| AU2021102747A4 (en) | A Municipal Wastewater Treatment Process Applicable to Quasi-Class IV Water Standard | |
| CN105776749B (en) | The catalysis oxidation that organic wastewater is electroplated combines polynary biochemical system and its deep treatment method | |
| CN107265791A (en) | Kitchen garbage slurry fermentation waste water processing unit | |
| CN214218490U (en) | Landfill leachate treatment system | |
| US20230312382A1 (en) | System and method for efficient nitrogen and carbon removal and phosphorus recovery of source-separated fresh urine by biochemical combination | |
| CN107973406A (en) | One kind realizes dirty Organic substance in water and the separated apparatus and method of ammonia nitrogen | |
| CN209835881U (en) | Distributed household type integrated sewage treatment device suitable for rural areas | |
| CN218811022U (en) | Integrated treatment device for deep denitrification of garbage penetration filtrate | |
| CN115367963A (en) | Percolate treatment process for small compression station | |
| CN212833299U (en) | Modularized long-term treatment device for excrement wastewater of toilet wastewater collector of railway train | |
| CN210340626U (en) | Blue algae deep dehydration wastewater treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |